575548 經濟部智慧財產局g(工消費合作杜印製 A7 ___ B7五、發明説明（1 ) 胃明所屬技術領域 本發明係關於可延長作爲觸媒所使用的酸性陽離子之 壽命的雙酚A製造方法，雙酚A作爲聚碳酸酯樹脂、環氧 基樹脂、聚烯丙酸樹脂等原料係爲有用的。 先前技術 已知雙酚A〔 2,2-雙（4-羥基苯基）丙烷〕爲，作爲聚 碳酸酯或工程塑質樹脂等之工學塑質，或環氧基樹脂等的 原料係爲重要化合物，近年來有逐漸增大其需求之傾向。 已知該雙酚A亦由，酸性陽離子交換樹脂觸媒及，若 必要爲烷基硫醇等硫磺化合物的助觸媒存在下，縮合丙酮 與過剩的酚而製造。酸性陽離子交換樹脂會經時性地劣化 。該主要劣化原因爲來自原料的重質物，由反應器的入口 邊即開始劣化。其劣化速度因快速，必須塡充過剩的觸媒 而長期連續運轉。觸媒的劣化一開始，欲維持生產量（維 持酚轉化率），供給於反應器的丙酮必須經時性地增加。 此時，反應器出口的未反應丙酮由蒸餾塔回收，故增加的 丙酮量會因蒸餾塔的能力而受到限制。即，到達蒸餾塔的 能力極限時必須換新觸媒。因此，反應條件適當地控制至 不增加丙酮量，且觸媒僅可長時間使用皆與減少製造成本 有關。而有一些目的雖相異但有關改良反應條件之公開專 利，例如特開昭54- 1 9952號公報、特開第2779952號公報、 特開平11-256458號公報、美國專利第4400555號說明書中記 載直列設置反應器，將羰基化合物分別添加於各反應器之 本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） (請先閲讀背面之注意事項再填寫本頁) -4- 575548 A7 B7 經濟部智慧財產局員工消費合作社印製 五、發明説明（2 ) 方法，但無到達有關延長酸性陽離子交換樹脂壽命之改良 〇 本發明提供一種雙酚A的製造方法，其由上述觀點所 成者，作爲觸媒所使用的酸性陽離子交換樹脂可延長壽命 者。 發明內容 經本發明者詳細硏究結果，發現直列連續的具有至少2 個反應帶區之反應裝置上，連續供給酚A與丙酮而製造雙 酚A的方法中，使用經特定部分性中和之酸性陽離子交換 樹脂，且因至少分爲2個反應帶區供給特定甲醇濃度的丙酮 ，可維持較高酚轉化率，而完成本發明。 即’本發明提供一種雙酚A的製造方法，其爲於成直 列連續的具有至少2個反應帶區之反應裝置上，連續供給酚 A與丙酮而製造雙酚A的方法，其特徵爲使用酸點的丨5〜 50%以含硫氮化合物進行部份中和之酸性陽離子交換樹脂 作爲觸媒，且甲醇濃度爲3,〇〇〇ppm以下之丙酮至少分爲2個 反應帶區而供給者。 貫施發明的最佳態樣 以下對本發明做詳細說明。 首先對雙酚A製造方法之步驟槪要做說明。 步驟（1 )(反應步驟） (請先閱讀背面之注意事項再填寫本頁) 本纸張尺度適用中.國國家標準（CNS ) A4規格（210X297公釐） -5- 575548 A7 B7 五、發明説明（3 ) (請先閲讀背面之注意事項再填寫本頁) 雙酚A係由，酸性陽離子交換樹脂作爲觸媒，若必要 使用烷基硫醇作爲助觸媒使用，反應丙酮與過剩的酚而製 造。作爲觸媒的酸性陽離子交換樹脂，一般使用磺酸型陽 離子交換樹脂，例如可舉出磺化苯乙烯•二乙烯苯共聚物 、磺化交聯苯乙烯聚合物、酚甲醛-磺酸樹脂、苯甲醛-磺酸 樹脂等。這些可單獨使用或組合2種以上使用。 反應混合物中，含有除雙酚A以外，未反應酚未反應 丙酮、觸媒、副生水、烷基硫醇、及有機硫磺化合物、著 色物質等副產物。 步驟（2 )(副生水、未反應原料的回收步驟） 其次，步驟（1 )所得之反應混合物，經由減壓蒸餾， 未反應丙酮、副生水及烷基硫醇等由塔頂除去，塔底得到 含有雙酚A及酚等液狀混合物。此時的減壓蒸餾條件，壓 力爲7〜80kPa，溫度爲70〜180°C範圍下實施，此時未反應 酚經共沸，其一部份由塔頂排除系統外。 經濟部智慧財產局員工消費合作社印製 步驟（3 )(雙酚A的濃縮步驟） 對反應混合物中除去如上述的物質之塔底液，酚由減 壓蒸餾除去，雙酚A被濃縮。該濃縮殘留液體作爲以下的 晶析原料。對於濃縮條件雖無特別限制，一般溫度爲1 〇〇〜 170°C，壓力爲5〜67kPa條件下進行。溫度若低於l〇〇°C時 需要尚真空，比1 7 0 °C尚時於以下的晶析步驟中需要多餘的 除熱步驟。又，濃酸殘液之雙酚A濃度爲20〜50質量％， 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） -6 - 575548 經濟部智慧財產局g(工消費合作社印製 A7 ____B7_五、發明説明（4 ) 較佳爲20〜40質量％範圍。該濃度若未達20質量％時雙酚A 的回收率低，若超過50質量％時晶析後的泥漿難以運送。 步驟（4 )(晶析步驟） 步驟（3)所得之濃酸殘液冷卻至40〜70°C，雙酚A與 酚之附加物（以下簡稱爲酚加合物）經晶析成爲泥漿狀。 冷卻經由加於外部熱交換器或晶析機的水經蒸發除熱而進 行。其次，泥漿狀的濃酸殘液經過濾、離心分離等由含有 酚加合物與反應副產物之晶析母液中分離。該晶液母液， 直接回收或回收一部分至反應器中，或一部份或全部經鹼 分解成爲酚與異丙烯基酚後回收。又，一部份或全部亦可 經異構化而回收於晶析原料中。 步驟（5 )(酚加合物之加熱熔融步驟） 步驟（4 )所得之雙酚A與酚之1 : 1加合物結晶於100 〜1 60°C下加熱熔融，成爲液狀混合物。 步驟（6 )(酚加合物之回收步驟） 由步驟（5 )所得之液狀混合物’經減壓蒸餾將酚除去 ，回收雙酚A。減壓蒸餾的條件爲壓力丨〜14kPa，溫度150 〜1 9 01：爲範圍。且已知經由蒸汽汽提將殘存的酚除去之方 法。 步驟（7 )(雙酚A的造粒步驟） (請先閱讀背面之注意事項再填寫本頁) 本紙張尺度適用中國國家標準（CNS ) A4規格（2丨〇><297公釐） 575548 A7 B7 五、發明説明（5 ) (請先閱讀背面之注意事項再填寫本頁) 步驟（6 )所得的熔融狀態之雙酚A，經由噴霧乾燥等 造粒裝置成爲液滴，成爲經冷卻固化之製品。液滴係由噴 霧、散步等而製得，由氮氣或空氣等而冷卻。 其次對本發明的方法作詳細說明。 本發明爲提供一種雙酚A的製造方法，其爲於成直列 連續的具有至少2個反應帶區之反應裝置上，連續供給酚A 與丙酮而製造雙酚A的方法，其特徵爲使用酸點的1 5〜50 %以含硫氮化合物進行部份中和之酸性陽離子交換樹脂作 爲觸媒’且甲醇濃度爲3,OOOppm以下之丙酮至少分爲2個反 應帶區而進行供給者。 作爲觸媒使用酸點的1 5〜50%以含硫氮化合物進行部 份中和之酸性陽離子交換樹脂。中和率或未達1 5 %時，觸 媒本身的耐甲醇性會降低，使丙酮分開供給的效果減少。 另一方面，中和率若超過5 0 %時，觸媒的活性會急速下降 而不佳。較佳爲20〜30%。 經濟部智慧財產局S工消費合作社印製 作爲使用於中和之含硫氮化合物，可舉出3-硫醇甲基 D比卩定、3 -硫醇乙基卩比卩定、2 -硫醇乙基舭Π定、4 -硫醇乙基D比π定 等吡啶鏈烷硫醇類、前述的吡啶鏈烷硫醇類與丙酮、甲基 乙基酮、甲基異丁基酮、乙醯酚、環己酮等酮所得之吡啶 鏈烷硫醇類、2-硫醇乙基胺、3_硫醇丁胺、3_正丙胺-i_丙 基硫醇等之胺鏈院硫醇類、t h i a ζ ο 1 y z i n e、2，2 -二甲基 thiazolyzine、環院基 thiazolyzine 等 thiazolyzine 類，其中 以2,2-二甲基thiazolyzine、2-硫醇乙基胺爲佳。 又，丙酮中甲醇濃度必須爲3,000ppm以下。若超過 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） -8- 575548 A7 B7 五、發明説明（6) 3，0 0 0 p p m，甲醇的影響爲顯著而不佳。較佳爲2，0 0 〇 p p m以 下。 對於反應溫度以6 0〜1 0 0 °C範圍爲佳。溫度未達6 0 °C時 ，酚相會固化，又若超過1 00°C時，離子交換樹脂的劣化會 增大而不佳。且較佳爲65〜95 °C的範圍。 對於酚/全丙酮（莫耳比），以6〜1 3的範圍爲佳。若未 達6時會有製品雙酚A之顏色不安定之情況。又，若超過i 3 時反應速度會變慢，酚的回收量會增加而不佳。較佳爲8〜 1 2的範圍。 對於各反應器的丙酮供給量，雖無特別限制，於第一 反應器中供給3 0〜5 0 %的丙酮，第二以後之反應則等分剩 下的丙酮而供給。使用三段反應時的流程圖如圖1所示。 且，各反應器的液態空間速度（LHSV)爲0.2-301^1 之範圍爲佳，較佳爲0.5〜6Η〆之範圍。 其次，本發明經由實施例做具體說明，但本發明不受 這些實施例之限制。 實施方式 〔實施例1〕 於各3塔的不鏽鋼管中塡充，以6 9 c c水膨潤的經2，2 -二 甲基t h i a ζ ο 1 y z i n e中和酸點的2 0 %之酸性陽離子交換樹脂（ 三菱化學公司製，Dayay〇nSK104)，反應溫度75°C下，酚 以277cc/hi·，丙酮以8 cc/hr分別由各塔入口供給。酚/全酮 (莫耳比）爲1 〇。又，所使用的丙嗣中甲醇濃度爲1，0 0 0 p p m 本纸張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） (請先閲讀背面之注意事項再填寫本頁) 訂 f 經濟部智慧財產局員工消費合作社印製 - 9- 575548 經濟部智慧財產局S工消費合作社印製 A7 __ B7五、發明説明（7 ) 。反應開始初期之第3塔出口之酚轉化率爲14.〇%，經過5〇〇 時間後爲12.8%。 〔比較例1〕 全丙酮一齊由第1塔目以24 cc/hr供給之外與實施例1相 同方法進行反應。反應開始初期之3塔出口之酚轉化率爲 14 · 0 % ’經過5 0 0時間後爲12 · 0 %。此與實施例1所得之1 2 · 8 %有著顯著差。 〔比較例2〕 使用離子交換樹脂中和率爲1 0%者之外與實施例1相同 方法進行反應。反應開始初期之3塔出口之酚轉化率爲14.0 %，經過500時間後爲11.2%。 〔比較例3〕 使用丙酮之甲醇濃度爲5,000ppm者之外與實施例1相同 進行反應。反應開始初期之3塔出口之酚轉化率爲14.0%， 經過500時間後爲11.8%。 產業上可利用性 本發明提供一種雙酚A的製造方法，其爲於成直列連 續的具有至少2個反應帶區之反應裝置上，連續供給酚A與 丙酮而製造雙酚A的方法，其特徵爲使用酸點的1 5〜50% 以含硫氮化合物進行部份中和之酸性陽離子交換樹脂作爲 本纸張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） (請先閲讀背面之注意事項再填寫本頁) 575548 A7 ___________B7_ 五、發明説明（8 ) 觸媒，且甲醇濃度爲3,000ppm以下之丙酮至少分爲2個反應 帶區而進行供給，可延長作爲觸媒的酸性陽離子交換樹脂 之壽命。 圖式簡單說明 圖1表示本發明方法的反應步驟之流程圖一例° A爲丙 酮、B爲酚、1爲第一反應器、2爲第二反應器及3爲第三反 應器。 (請先閲讀背面之注意事項再填寫本頁} 衣. -訂 f 經濟部智慧財產局員工消費合作社印製 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） -11 -575548 Bureau of Intellectual Property, Ministry of Economic Affairs (manufactured by industrial and consumer cooperation, printed A7 ___ B7 V. Description of invention (1) Weiming Technical Field The present invention relates to the manufacture of bisphenol A that can extend the life of acid cations used as catalysts In the method, bisphenol A is useful as a raw material system of polycarbonate resin, epoxy resin, polyallylic acid resin, etc. Bisphenol A [2,2-bis (4-hydroxyphenyl) propane] is known in the prior art. In order to increase the demand for engineering plastics such as polycarbonates and engineering plastic resins, or raw materials based on epoxy resins, the demand has gradually increased in recent years. In the presence of an acidic cation exchange resin catalyst and, if necessary, a promoter of a sulfur compound such as an alkyl mercaptan, it is produced by condensing acetone with an excess of phenol. The acidic cation exchange resin deteriorates over time. The main cause of deterioration It is a heavy material from the raw material, and it starts to deteriorate at the entrance side of the reactor. The deterioration rate is fast, and it must be filled with excess catalyst and run continuously for a long time. At the beginning of the deterioration of the catalyst, it is necessary to maintain the production volume (dimensional Phenol conversion rate), the acetone supplied to the reactor must be increased over time. At this time, the unreacted acetone at the reactor outlet is recovered by the distillation column, so the increased amount of acetone will be limited by the capacity of the distillation column. That is, When the capacity limit of the distillation column is reached, a new catalyst must be replaced. Therefore, the reaction conditions are appropriately controlled so as not to increase the amount of acetone, and the catalyst can only be used for a long time, which is related to reducing the manufacturing cost. Although some purposes are different, they are related Published patents for improving reaction conditions are described in, for example, Japanese Patent Application Laid-Open No. 54-19592, Japanese Patent Application No. 2779952, Japanese Patent Application Laid-Open No. 11-256458, and US Patent No. 4400555. The paper size added to each reactor is applicable to China National Standard (CNS) A4 specifications (210X 297 mm) (Please read the precautions on the back before filling this page) -4- 575548 A7 B7 Employees ’Intellectual Property Bureau, Ministry of Economic Affairs Cooperative prints 5. Description of the invention (2) method, but no improvement related to extending the life of the acidic cation exchange resin is achieved. The present invention provides a dual A method for producing phenol A, which is formed by the above-mentioned viewpoints, is an acidic cation exchange resin used as a catalyst that can prolong the life. SUMMARY OF THE INVENTION The present inventors have studied the results in detail and found that there are at least two reaction zones in a straight line. In the method for producing bisphenol A by continuously supplying phenol A and acetone on the reaction device, an acidic cation exchange resin neutralized by a specific partial is used, and acetone with a specific methanol concentration is supplied because it is divided into at least two reaction zones. The present invention can be completed while maintaining a high phenol conversion rate. That is, the present invention provides a method for producing bisphenol A, which continuously supplies phenol A and phenol A to a reaction device having at least two reaction zones in a continuous row. A method for producing bisphenol A by using acetone, which is characterized by using an acidic cation exchange resin having a neutral point of 5 to 50% and a sulfur-nitrogen-containing compound as a catalyst, and a methanol concentration of 3,000 ppm. The following acetone is supplied to at least two reaction zone regions. Best Mode for Carrying Out the Invention The present invention will be described in detail below. First, the steps of the method for producing bisphenol A will be explained. Step (1) (Reaction step) (Please read the precautions on the back before filling out this page) The paper size is applicable. National Standard (CNS) A4 (210X297 mm) -5- 548548 A7 B7 V. Invention Note (3) (Please read the notes on the back before filling this page) Bisphenol A is based on acidic cation exchange resin as the catalyst, if necessary, alkyl mercaptan is used as a catalyst to react acetone with excess phenol While manufacturing. As the acidic cation exchange resin used as a catalyst, a sulfonic acid type cation exchange resin is generally used. Examples thereof include a sulfonated styrene-divinylbenzene copolymer, a sulfonated crosslinked styrene polymer, a phenol formaldehyde-sulfonic acid resin, and benzene. Formaldehyde-sulfonic resin and so on. These can be used individually or in combination of 2 or more types. The reaction mixture contains by-products other than bisphenol A, unreacted phenol, unreacted acetone, catalyst, by-product water, alkyl mercaptan, organic sulfur compounds, and colored substances. Step (2) (Recovery step of by-product water and unreacted raw materials) Next, the reaction mixture obtained in step (1) is subjected to distillation under reduced pressure, and unreacted acetone, by-product water, and alkyl mercaptan are removed from the top of the column. A liquid mixture containing bisphenol A and phenol was obtained at the bottom of the column. The reduced pressure distillation conditions at this time are carried out at a pressure of 7 to 80 kPa and a temperature of 70 to 180 ° C. At this time, the unreacted phenol is azeotropically, and a part of it is excluded from the system by the top of the column. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs Step (3) (Concentration step of bisphenol A) The bottom liquid of the above-mentioned substance is removed from the reaction mixture, the phenol is removed by vacuum distillation, and the bisphenol A is concentrated. This concentrated residual liquid was used as the following crystallization raw materials. Although there are no particular restrictions on the concentration conditions, it is generally performed at a temperature of 100 to 170 ° C and a pressure of 5 to 67 kPa. If the temperature is lower than 100 ° C, a vacuum is required. If it is lower than 170 ° C, the following crystallization step requires an extra heat removal step. In addition, the concentration of bisphenol A in the concentrated acid residue is 20-50% by mass. The size of this paper applies the Chinese National Standard (CNS) A4 specification (210X297 mm) -6-575548. Intellectual Property Bureau of the Ministry of Economic Affairs. Preparation of A7 ____B7_ V. Description of the invention (4) It is preferably in the range of 20 to 40% by mass. If the concentration is less than 20% by mass, the recovery rate of bisphenol A is low, and if it exceeds 50% by mass, the slurry after crystallization is difficult. The step (4) (crystallization step) The concentrated acid residue obtained in step (3) is cooled to 40 to 70 ° C, and the bisphenol A and phenol addition (hereinafter referred to as phenol adduct) is crystallized into Slurry-like. Cooling is performed by removing heat from the water added to an external heat exchanger or crystallizer. Second, the concentrated acid-like residue in the slurry is filtered, centrifuged, etc. Separation from the crystallization mother liquor. The mother liquor of the crystallization solution is directly recovered or recovered into the reactor, or a part or all of the mother liquor is recovered after being decomposed into phenol and isopropenylphenol. Moreover, a part or all of the crystallization mother liquor can also be recovered. Isomerized and recovered in the crystallization raw material. Step (5) (phenol adduct Step of heating and melting) The 1: 1 adduct of bisphenol A and phenol obtained in step (4) is heated and melted at 100 ~ 1 60 ° C to become a liquid mixture. Step (6) (Recovery of phenol adduct Step) The liquid mixture obtained in step (5) 'is subjected to reduced pressure distillation to remove phenol and recover bisphenol A. The conditions for the reduced pressure distillation are a pressure of ~ 14 kPa and a temperature of 150 to 1 9 01: the range is known. Method for removing residual phenol by steam stripping. Step (7) (Granulation step of bisphenol A) (Please read the precautions on the back before filling in this page) The paper size applies to Chinese National Standard (CNS) A4 (2 丨 〇 > < 297 mm) 575548 A7 B7 V. Description of the invention (5) (Please read the precautions on the back before filling this page) The bisphenol A in the molten state obtained in step (6) is sprayed Granulation devices such as drying become liquid droplets and become solidified products after cooling. The liquid droplets are made by spraying, walking, etc., and are cooled by nitrogen or air. Next, the method of the present invention is described in detail. The present invention provides a method Method for producing bisphenol A in line A method for producing bisphenol A by continuously supplying phenol A and acetone to a continuous reaction device having at least two reaction zones, which is characterized in that it partially neutralizes with sulfur nitrogen compounds using 15 to 50% of the acid point. The acidic cation exchange resin is used as a catalyst, and the acetone with a methanol concentration of 3,000 ppm or less is divided into at least two reaction zone regions. The catalyst is supplied using 15 to 50% of the acid point of the sulfur-nitrogen-containing compound. Partially neutralized acidic cation exchange resin. When the neutralization rate is less than 15%, the methanol resistance of the catalyst itself will be reduced, and the effect of separate supply of acetone will be reduced. On the other hand, if the neutralization rate exceeds 50%, the activity of the catalyst will decrease rapidly and become unfavorable. It is preferably 20 to 30%. Printed as a sulfur-containing nitrogen compound for neutralization by the Intellectual Property Bureau of the Intellectual Property Bureau of the Ministry of Economic Affairs. Examples include 3-thiol methyl D ratio, 3-thiol ethyl ratio, and 2-sulfur. Pyridine alkane thiols such as alcohol ethyl hydrazone, 4-thiol ethyl D to π ratio, the aforementioned pyridine alkane thiols and acetone, methyl ethyl ketone, methyl isobutyl ketone, ethyl Pyridine alkane thiols obtained from ketones such as phenol and cyclohexanone, amine chain thiols such as 2-thiol ethylamine, 3-thiol butylamine, 3-n-propylamine-i-propylthiol, etc. Thiazolyzine, thia ζ ο 1 yzine, 2,2-dimethylthiazolyzine, and cyclothiazylzine, among which 2,2-dimethylthiazolyzine and 2-thiol ethylamine are preferred. The methanol concentration in acetone must be 3,000 ppm or less. If it exceeds the standard of this paper, the Chinese National Standard (CNS) A4 specification (210X297 mm) is applied. -8- 575548 A7 B7 V. Description of the invention (6) 3, 0 0 0 p p m, the effect of methanol is significant and not good. Preferably, it is 2,000 p p m or less. The reaction temperature is preferably in the range of 60 to 100 ° C. When the temperature is less than 60 ° C, the phenol phase will be cured, and if it exceeds 100 ° C, the deterioration of the ion exchange resin will increase and is not good. The temperature is preferably in the range of 65 to 95 ° C. For phenol / peracetone (molar ratio), a range of 6 to 13 is preferable. If it is less than 6, the color of the product bisphenol A may be unstable. In addition, if i 3 is exceeded, the reaction rate is slowed, and the recovery amount of phenol is increased to be unfavorable. The range of 8 to 12 is preferable. Although the supply amount of acetone in each reactor is not particularly limited, 30 to 50% of acetone is supplied in the first reactor, and the remaining acetone is divided into equal parts and supplied in the second and subsequent reactions. The flow chart when using a three-stage reaction is shown in Figure 1. In addition, the liquid space velocity (LHSV) of each reactor is preferably in the range of 0.2-301 ^ 1, and more preferably in the range of 0.5-6 Η〆. Next, the present invention is specifically described by way of examples, but the present invention is not limited by these examples. Embodiment [Example 1] Fill 3 stainless steel tubes with 3 towers, and swell with 6 9 cc of water to neutralize acidic cations with 20% of acid point by 2,2-dimethylthia ζ ο 1 yzine Resin (manufactured by Mitsubishi Chemical Corporation, DayayOnSK104), at a reaction temperature of 75 ° C, phenol was supplied at 277 cc / hi · and acetone was supplied at 8 cc / hr from the inlet of each column. The phenol / perone (mole ratio) was 10. In addition, the methanol concentration in the used propionate is 1,000 ppm. This paper size is applicable to the Chinese National Standard (CNS) A4 specification (210X 297 mm) (Please read the precautions on the back before filling this page). f Printed by the Consumers 'Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs-9- 575548 Printed by the Consumers' Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs A7 __ B7 V. Description of Invention (7). The phenol conversion rate at the exit of the third tower at the beginning of the reaction was 14.0%, and 12.8% after 5000 hours. [Comparative Example 1] Reaction was carried out in the same manner as in Example 1 except that all of the acetone was supplied from the first mesh at 24 cc / hr. The phenol conversion rate at the exit of the 3 towers at the beginning of the reaction was 14.0%, and 12.0% after 5 hours. This is significantly different from the 12 · 8% obtained in Example 1. [Comparative Example 2] A reaction was carried out in the same manner as in Example 1 except that the neutralization rate of the ion exchange resin was 10%. The phenol conversion rate at the exit of the 3 towers at the beginning of the reaction was 14.0%, and after 500 hours, it was 11.2%. [Comparative Example 3] A reaction was carried out in the same manner as in Example 1 except that the methanol concentration of acetone was 5,000 ppm. The phenol conversion rate at the exit of the 3 towers at the beginning of the reaction was 14.0% and after 1 hour, it was 11.8%. INDUSTRIAL APPLICABILITY The present invention provides a method for producing bisphenol A, which is a method for producing bisphenol A by continuously supplying phenol A and acetone on a reaction device having at least two reaction zones in a continuous line, It is characterized by the use of 15 ~ 50% of acid point and acidic cation exchange resin partially neutralized with sulfur-containing nitrogen compounds as the paper standard. Applicable to China National Standard (CNS) A4 specification (210X297 mm) (please read the back first) Please note this page and fill in this page again) 575548 A7 ___________B7_ V. Description of the invention (8) Catalysts and acetone with a methanol concentration of 3,000ppm or less are supplied by at least 2 reaction zones, which can extend the acidic cations as catalysts Life of exchange resin. Brief description of the drawings Figure 1 shows an example of a flow chart of the reaction steps of the method of the present invention. A is acetone, B is phenol, 1 is the first reactor, 2 is the second reactor, and 3 is the third reactor. (Please read the precautions on the back before filling this page} Clothes.-Order f Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs This paper size applies to China National Standard (CNS) A4 (210X297 mm) -11-